CN218232078U - System for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production - Google Patents
System for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production Download PDFInfo
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Abstract
The utility model discloses a system for recovering sulfur and ammonia nitrogen in waste water of thio-carbazide production, which comprises an oxidation part, a filtering part, a pH adjusting part and a stripping tower, wherein the oxidation part comprises an oxidation tower and an aeration column therein, an oxidation gas inlet is connected with the aeration column through an air inlet pipe, an oxidation liquid outlet is arranged at the bottom of the oxidation tower, and effluent is filtered by a bag filter of the filtering part; the filtered water is connected with a mixer of the pH adjusting part, and the filtered water is connected with a stripping tower; the top of the stripping tower is provided with an ammonia outlet, and the bottom of the stripping tower is provided with an external drainage outlet. The device can effectively improve the treatment effect, the treatment stability and the adaptability of the wastewater produced by the thiocarbohydrazide, effectively reduce the operation cost of the wastewater produced by the thiocarbohydrazide, and realize the effective recovery of resources while treating the wastewater.
Description
Technical Field
The utility model belongs to industrial wastewater treatment technology and resource recovery field, concretely relates to system for retrieving sulphur and ammonia nitrogen in thio-carbazide industrial waste water.
Background
The waste water is a general term of water discharged in the process of resident activities and runoff rainwater, and comprises domestic sewage, industrial waste water and other useless water flowing into a drainage pipe canal from initial rainwater, generally refers to water which can not be recycled after certain technical treatment or can not reach a certain standard after primary pollution, namely thiocarbamoyl hydrazine, also called thiocarbamoyl hydrazine, thiocarbamoyl urea, homodiaminothiourea, 1, 3-diaminothiourea and N, N-bis- (2, 4-dimethyl imino methyl) methylamine, is widely used for organic synthesis, is an important production raw material of high-efficiency broad-spectrum herbicide-metribuzin, and can generate a large amount of waste water with COD as high as 250000mg/L, ammonia nitrogen amount as high as 70000mg/L, sulfur content as high as 40000mg/L and pH value of 11-14.
The current commonly used method for treating wastewater is a chemical precipitation method, namely, lime is used for adjusting the pH value of the wastewater, and a metal collecting agent is added for neutralization, coagulation, flocculation and precipitation. Further, there are ion exchange method, adsorption method, electrodialysis method, evaporation concentration method, reverse osmosis method and the like. For example, CN210559492U discloses a wastewater treatment device for thiocarbohydrazide production, the main principle is that waste water is treated by an adsorption filtration mode, and the method not only has poor treatment effect, but also wastes resources and generates secondary pollution. CN201810747298.0 discloses a thiocarbazide production wastewater treatment process, ammonia nitrogen is taken out by stirring and heating and dilute sulfuric acid absorption, and sulfur is removed by adding dilute sulfuric acid for reaction. According to the experiment through the mode of stirring ammonia nitrogen of hardly effectively taking out the aquatic, simultaneously because waste water is the strong basicity, need throw with a large amount of sulphuric acid, can lead to aquatic salinity increase simultaneously, not only the treatment effect is poor, the waste water treatment's that still increases the degree of difficulty.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the existing treatment method, the invention aims to provide a system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production, which has the advantages of quick treatment effect, stable effect, wider adaptability and lower cost.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production, which comprises an oxidation part, a filtering part, a pH adjusting part and a stripping tower 9,
the oxidation part comprises an oxidation tower 3 and an aeration column 302 in the oxidation tower, the oxidation tower 3 comprises a waste water inlet, an oxidation gas inlet is connected with the aeration column 302 through an air inlet pipe penetrating through the wall of the oxidation tower 3, the bottom of the oxidation tower 3 is provided with an oxidation liquid outlet,
the filtering part comprises a bag filter, the oxidizing liquid outlet is connected with the inlet of the bag filter, the bottom of the bag filter is provided with a filtrate outlet,
the pH adjusting part comprises a mixer 603, an inlet of the mixer 603 is connected with the filtrate outlet, an outlet of the mixer 603 is connected with an inlet of the stripping tower 9, an ammonia gas outlet is arranged at the top of the stripping tower 9, and an external drainage outlet is arranged at the bottom of the stripping tower 9.
Further, a gas filter 2 is arranged between the oxidizing gas inlet and the aeration column, and is used for pretreating a gas source to provide a high-efficiency stable gaseous oxidant for the oxidation tower 3.
The oxidizing gas is one or more of ozone, air or oxygen, and most preferably air.
Said oxygenThe gas inflow of the gas is 2-5 m 3 The pressure of inlet gas is 0.3-0.5MPa.
The impurity removed by the gas filter 2 is CO 2 One or more of water vapor, dust or nitrogen oxides.
Furthermore, the air inlet pipe is in a vertical inverted U shape outside the oxidation tower, and the top of the air inlet pipe is 0-1 m higher than the top of the oxidation tower 3.
Further, the system for recovering sulfur and ammonia nitrogen in the wastewater from the thiocarbohydrazide production further comprises a wastewater storage tank 1, and an outlet of the wastewater storage tank 1 is connected with the wastewater inlet. The waste water storage tank 1 is used for storing and outputting thiocarbohydrazide waste water.
Further, a pump is arranged between the waste water storage tank 1 and the oxidation tower 3.
Further, the oxidation tower 3 further comprises a jacket 303 arranged on the periphery.
Further, the effective height of the jacket 303 covering the oxidation tower 3 is 1/3-1/2.
Further, the medium in the jacket 303 is one of low-pressure steam, hot water or hot oil.
Further, the temperature of the medium in the jacket 303 is 50-120 ℃.
Further, the aperture of the aeration column 302 is 0.1 to 10 μm.
Further, the wastewater inlet is positioned between 1/2 and 4/5 of the height of the oxidation tower 3.
Further, the air inlet of the aeration column 302 is positioned between 1/4 and 1/2 of the height of the oxidation tower 3.
Further, the top of the oxidation tower 3 is also provided with an air outlet.
Further, the oxidation tower 3 further comprises a viewing mirror arranged at the oxidation liquid outlet.
Further, the oxidation tower 3 also comprises a viewing mirror arranged between 3/4 and 4/5 of the height of the oxidation tower.
Furthermore, the filtering part comprises 2-4 groups of bag type filters connected in parallel. The bag filters arranged in parallel can be controlled by respective valves to realize alternate work, and the byproduct sulfur is removed while the filtration is uninterrupted.
Furthermore, the aperture of the filter bag of the bag filter is 400-800 meshes.
Further, a sight glass is arranged at the filtrate outlet.
Further, the filtering part also comprises a back washing pipeline connected with the bag filter, and the filtrate outlet is connected with the waste water storage tank 1 through a pipeline. The flushing water generated in the back flushing process flows back into the waste water storage tank.
Further, the inlet and the filtrate outlet of the bag filter are both provided with a pressure transmitter. When the differential pressure of the pressure transmitter reaches 0.3-0.5MPa, the bag filter is backwashed by the backwashing pipeline.
The back washing time is 1-3 h.
The water for back washing is standard external drainage, industrial water or tap water.
Further, the pH adjusting part further includes a lye tank 6, and an outlet of the lye tank 6 is connected to the mixer 603.
Further, the lye tank is connected to the mixer 603 through a pump.
Further, the mixer 603 is a tube mixer. So as to realize the full mixing of the medicament and the wastewater.
Further, a first pH transmitter 604 is disposed at an outlet of the mixer 603. The first pH transmitter controls the pH of the effluent of the mixer 603 to be 9-14.
The mass concentration of the alkali liquor in the alkali liquor tank is 8-30%.
Further, the system for recovering sulfur and ammonia nitrogen in the wastewater from the production of thiocarbohydrazide further comprises an intermediate water storage tank 7, wherein the intermediate water storage tank 7 is positioned between the mixer 603 and the stripping tower 9.
Further, a second pH transmitter 701 and a pump are arranged at the outlet of the intermediate water storage tank 7, and the second pH transmitter 701 controls the operation of the pump. When the pH of the outlet water of the intermediate water storage tank 7 is 9 to 14, the second pH transmitter 701 controls the pump to deliver the intermediate water to the stripping tower 9.
Further, a heat exchanger 8 is arranged in front of an inlet of the stripping tower 9, and the external water of the stripping tower 9 exchanges heat with the wastewater before entering the stripping tower 9 through the heat exchanger 8. The device is used for realizing the collection and the reutilization of the waste heat of the discharged water and the temperature control of the discharged water.
Further, the system for recovering sulfur and ammonia nitrogen in the wastewater from the production of thiocarbohydrazine further comprises a condenser 11, wherein an ammonia gas outlet is connected with the condenser 11, and an outlet of the condenser 11 is connected with an ammonia water storage tank 10. The ammonia water storage tank is used for storing and recovering the condensed ammonia water. The gas medium of the stripping tower 9 is steam with the temperature of 120-160 ℃, and the steam flow is 200-500kg/h.
Further, the outer drainage outlet is connected with the stripping tower 9 through a wastewater circulating pipeline, an ammonia nitrogen detector 908 is arranged at the wastewater circulating pipeline, and the wastewater circulating pipeline is connected with the drainage outlet through a branch pipe and a valve. Through ammonia nitrogen detector 908 control valve, when ammonia nitrogen exceeds standard, make waste water form the circulation through control valve, after ammonia nitrogen is up to standard, make the play water discharge after heat exchanger 8 carries out the heat transfer through control valve.
Furthermore, the temperature of the outlet water of the heat exchanger 8 is controlled to be 30-35 ℃ by a temperature transmitter.
Further, the condenser 11 controls the temperature of the condensation water outlet to be 25-35 ℃ through a temperature transmitter. The condensing efficiency of the condenser is 99-99.99%. Further, the filtrate outlet is connected to the aeration column 302 through a pipeline and a valve, so as to perform back washing on the aeration column. When the pressure in the pipeline is lower than 0.2MPa, the valve is opened, and filtered water is used for backwashing the aeration column.
Pumping the wastewater produced in the production of the thiocarbohydrazide into an oxidation tower through a wastewater storage tank for treatment for a certain time to form a mixed solution of the wastewater and sulfur, pumping the mixed solution into a bag filter through a water pump, separating and recovering sulfur in the wastewater by the bag filter, taking the recovered sulfur as a byproduct, and switching alternate use of the bag filter through the pressure difference between the inlet and the outlet of the bag filter in the filtering process, for example, when 2 parallel bag filters are used, the bag filter 1 stops being used, the bag filter 2 starts to operate, a backwashing system of the bag filter 1 is started, backwashing is carried out on the bag filter 1, backwashing effluent flows back to the wastewater storage tank, and the steps are repeated in this way. And (3) adjusting the pH value of the separated filtrate in the mixer, then feeding the filtrate into a stripping tower, separating ammonia nitrogen in the intermediate wastewater by the stripping tower to form ammonia saturated steam, and allowing the ammonia saturated steam to flow out from an air outlet of the stripping tower. The condenser enables ammonia saturated water vapor to form ammonia water byproduct, and the ammonia water byproduct is recycled to the ammonia water storage tank. The wastewater for removing ammonia nitrogen is discharged after being detected to be qualified by the ammonia nitrogen detector of the stripping tower, and the wastewater discharged by the high-temperature stripping tower reaches the discharge standard after reaching the discharge temperature through the heat exchanger.
Drawings
FIG. 1 is a schematic structural diagram of the system for recovering sulfur and ammonia water from sulfur card wastewater.
Wherein: 1 is a waste water storage tank, 2 is a gas filter, 3 is an oxidation tower, 4, 5 are bag filters, 6 is an alkali liquor tank, 7 is an intermediate water storage tank, 8 is a heat exchanger, 9 is a stripping tower, 10 is an ammonia water storage tank, 11 is a condenser, 101, 306, 602, 702, 903 are all pumps, 301, 304, 4/503, 4/506 are all sight glasses, 305, 308, 401, 402, 404, 405, 501, 502, 504, 505, 4/504, 4/505, 4/507, 601, 904, 905, 906, 907 are all valves, 307, 4/501, 4/502, 901 are all pressure transmitters, 302 is an aeration column, 303 is a jacket, 403, 503 are all filter bags; 603 is a mixer, 604 is a first pH transmitter, 701 is a second pH transmitter, 801, 902 and 1101 are temperature transmitters, and 908 is an ammonia nitrogen detector.
Detailed Description
As shown in fig. 1, a system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production, includes an oxidation part, a filtering part, a pH adjusting part and a stripping tower 9, where the oxidation part includes an oxidation tower 3 and an aeration column 302 in the oxidation tower, the oxidation tower 3 includes a wastewater inlet, an oxidation gas inlet is connected to the aeration column 302 through an air inlet pipe passing through a wall of the oxidation tower 3, the bottom of the oxidation tower 3 is provided with an oxidation liquid outlet, the filtering part includes a bag filter, the oxidation liquid outlet is connected to an inlet of the bag filter, a filtrate outlet is provided at the bottom of the bag filter, the pH adjusting part includes a mixer 603, an inlet of the mixer 603 is connected to the filtrate outlet, an outlet of the mixer 603 is connected to an inlet of the stripping tower 9, the top of the stripping tower 9 is provided with an ammonia gas outlet, and the bottom of the stripping tower 9 is provided with an external drainage outlet.
And a gas filter 2 is arranged between the oxidizing gas inlet and the aeration column and used for pretreating a gas source to provide a high-efficiency stable gaseous oxidant for the oxidation tower 3.
The oxidizing gas is one or more of ozone, air or oxygen, and most preferably air.
The inlet flow rate of the oxidizing gas is 2-5 m 3 The pressure of inlet gas is 0.3-0.5MPa.
The impurity removed by the gas filter 2 is CO 2 One or more of water vapor, dust or nitrogen oxides.
The air inlet pipe is in a vertical inverted U shape outside the oxidation tower, and the top of the air inlet pipe is 0-1 m higher than the top of the oxidation tower 3.
The system for recovering sulfur and ammonia nitrogen in the wastewater from the production of thiocarbohydrazide further comprises a wastewater storage tank 1, and an outlet of the wastewater storage tank 1 is connected with the wastewater inlet. The waste water storage tank 1 is used for storing and outputting thiocarbohydrazide waste water.
A pump is arranged between the waste water storage tank 1 and the oxidation tower 3.
The oxidation tower 3 further comprises a jacket 303 arranged on the periphery.
The effective height of the jacket 303 covering the oxidation tower 3 is 1/3-1/2.
The medium in the jacket 303 is one of low-pressure steam, hot water or hot oil.
The temperature of the medium in the jacket 303 is 50-120 ℃.
The aperture of the aeration column 302 is 0.1-10 μm.
The wastewater inlet is positioned between 1/2 and 4/5 of the height of the oxidation tower 3.
The air inlet of the aeration column 302 is positioned between 1/4 and 1/2 of the height of the oxidation tower 3.
And the top of the oxidation tower 3 is also provided with an air outlet.
The oxidation tower 3 further comprises a sight glass arranged at the oxidation liquid outlet.
The oxidation tower 3 also comprises a viewing mirror arranged between 3/4 and 4/5 of the height of the oxidation tower.
The filtering part comprises 2-4 groups of bag filters connected in parallel. The bag filters arranged in parallel can be controlled by respective valves to realize alternate work, and the byproduct sulfur is removed while uninterrupted filtration is performed.
The aperture of the filter bag of the bag filter is 400-800 meshes.
A sight glass is arranged at the filtrate outlet.
The filtering part also comprises a back washing pipeline connected with the bag filter, and the filtrate outlet is connected with the wastewater storage tank 1 through a pipeline. The flushing water produced in the backwashing process flows back into the wastewater storage tank.
And pressure transmitters are arranged at the inlet of the bag filter and the filtrate outlet. When the differential pressure of the pressure transmitter reaches 0.3-0.5MPa, the bag filter is backwashed by the backwashing pipeline.
The back washing time is 1-3 h.
The water for backwashing is standard external drainage, industrial water or tap water.
The pH adjusting part also comprises an alkali liquor tank 6, and the outlet of the alkali liquor tank 6 is connected with the mixer 603.
The lye tank is connected to the mixer 603 via a pump.
The mixer 603 is a tube mixer. So as to realize the full mixing of the medicament and the wastewater.
A first pH transmitter 604 is arranged at the outlet of the mixer 603. The first pH transmitter controls the pH of the effluent of the mixer 603 to be 9-14.
The mass concentration of the alkali liquor in the alkali liquor tank is 8-30%.
The system for recovering sulfur and ammonia nitrogen in the wastewater from the production of thiocarbohydrazide further comprises an intermediate water storage tank 7, wherein the intermediate water storage tank 7 is positioned between the mixer 603 and the stripping tower 9.
The outlet of the intermediate water storage tank 7 is provided with a second pH transmitter 701 and a pump, and the second pH transmitter 701 controls the operation of the pump. When the pH of the outlet water of the intermediate water storage tank 7 is 9-14, the second pH transmitter 701 controls the pump to convey the intermediate water to the stripping tower 9.
A heat exchanger 8 is arranged in front of an inlet of the stripping tower 9, and the discharged water of the stripping tower 9 exchanges heat with the wastewater before entering the stripping tower 9 through the heat exchanger 8. The waste heat recycling device is used for realizing the collection and reutilization of waste heat of the discharged water and the temperature control of the discharged water.
The system for recovering sulfur and ammonia nitrogen in the waste water of the thiocarbohydrazide production further comprises a condenser 11, wherein an ammonia gas outlet is connected with the condenser 11, and an ammonia water storage tank 10 is connected with an outlet of the condenser 11. The ammonia water storage tank is used for storing and recovering the condensed ammonia water.
The gas medium of the stripping tower 9 is steam with the temperature of 120-160 ℃, and the steam flow is 200-500kg/h.
The outer drainage outlet is connected with the stripping tower 9 through a wastewater circulating pipeline, an ammonia nitrogen detector 908 is arranged at the wastewater circulating pipeline, and the wastewater circulating pipeline is connected with the drainage outlet through a branch pipe and a valve. Through ammonia nitrogen detector 908 control valve, when ammonia nitrogen exceeds standard, make waste water form the circulation through control valve, after the ammonia nitrogen is up to standard, make the play water discharge after heat exchanger 8 carries out the heat transfer through control valve.
The temperature of the outlet water of the heat exchanger 8 is controlled to be 30-35 ℃ by a temperature transmitter.
The condenser 11 controls the temperature of a condensation water outlet to be 25-35 ℃ through a temperature transmitter. The condensing efficiency of the condenser is 99-99.99%.
The filtrate outlet is connected with the aeration column 302 through a pipeline and a valve for back flushing the aeration column. When the pressure in the pipeline is lower than 0.2MPa, the valve is opened, and filtered water is used for back flushing the aeration column.
The method comprises the steps of pumping thiocarbazide production wastewater into an oxidation tower 3 through a wastewater storage tank 1 by a pump 101, treating gas by a gas filter 2, then feeding the gas into the oxidation tower 3, introducing a heat source into the oxidation tower 3 through a heating jacket 303 to heat the oxidation tower 3, treating the thiocarbazide production wastewater by fine oxidation bubbles generated by an aeration column 302, observing the reaction state through a sight glass 304, reacting for a certain time to form a mixed solution of wastewater and sulfur, pumping the mixed solution into a bag filter 4 through a pump 306, attaching a small amount of sulfur particles to the surface of the aeration column 302 after long-time operation, flushing the aeration column 302 through a pressure change control valve 308 switch of a pressure transmitter 307, separating and recovering sulfur in the wastewater by the bag filter 4, taking the recovered sulfur as a byproduct, switching the bag filter 4 and a pressure difference of an inlet and an outlet of the bag filter 4/501 and a pressure difference of 4/502 for alternate use, closing the valves 402 and 404 when the pressure difference reaches a certain value, opening the bag filters 401, 405, 502, 504 and 4/504, stopping use of the bag filter 5, starting operation of the bag filter 4, starting a backwashing system, and returning effluent to the bag filter 4, and thus performing reciprocating circulation. And pumping the separated wastewater into an intermediate water storage tank, closing a valve 4/504 and opening a valve 4/505 when sulfur particles are not contained by observing a sight glass 4/503, and enabling the subsequent wastewater to enter the intermediate storage tank, and repeating the steps in a circulating manner. The filtered water enters the intermediate water storage tank 7. During the process that the filtered water enters the intermediate water storage tank, the pump 602 and the valve 601 are controlled by the first pH transmitter 604, and the caustic soda liquid in the caustic soda liquid tank 6 is pumped into the mixer 603 to adjust the pH of the filtered water. Waste water detects through second pH changer 701 and reaches the back of requiring in the middle water storage tank 7, go into strip tower 9 through pump 702, the pump income process is through heat exchanger 8, realize preheating of middle waste water, strip tower 9 realizes the separation of ammonia nitrogen in the middle waste water through high temperature steam, form aqueous ammonia saturated vapor, aqueous ammonia saturated vapor flows to condenser 11 through strip tower 9 gas outlet, condenser 11 passes through outlet temperature changer controlled temperature, form the aqueous ammonia by-product and retrieve to aqueous ammonia storage tank 10. Through opening pump 903, valve 905, 906, valve 907 cut to the supreme expert, realize the circulation of outer drainage, through ammonia nitrogen detector 908, wait to detect qualified back, close valve 905, 906, valve 907 cuts to the right side, opens valve 904, and outer drainage carries out the heat transfer through heat exchanger 8, and the temperature of discharging water when up to standard is got rid of waste water through temperature transmitter 801 control, and outer drainage ammonia nitrogen and sulphide all can be up to standard this moment.
Example 1
In the experiment, the thiocarbohydrazide production wastewater is selected, the water amount is 50t/d, the ammonia nitrogen concentration is measured to be 75000mg/L, the sulfide content is 42000mg/L, the pH value is 12, and the experiment is carried out by controlling the air inflow to be 4m 3 L, the air inlet pressure is 0.3MPa, the temperature of the oxidation tower is 35 ℃, the aperture of the oxidation column is 4 mu m, the temperature of a heating jacket is controlled to be 50 ℃, and the reaction time is 5 hours; when the aperture of a filter bag of the bag filter 2 group is controlled to be 700 meshes, the steam temperature of the stripping tower is controlled to be 140 ℃, the steam quantity is 400kg/h, the water outlet temperature of the heat exchanger is controlled to be 30 ℃, the water outlet temperature of the condenser is controlled to be 30 ℃, and the pH value of the intermediate water storage tank is 13, the experiment is carried out by the implementation mode, the byproduct sulfur is effectively recovered by the experiment to be 2095kg/d, the 20% ammonia water is 30.3t/d, and the sulfide and ammonia nitrogen of the effluent reach the standard.
Example 2
The test selects the wastewater from the production of the thiocarbohydrazide, the water amount is 20t/d, the ammonia nitrogen concentration is measured to be 69000mg/L, the sulfide content is 40000mg/L, the pH value is 11, and the experiment controls the air inlet flow to be 3m 3 The reaction time is 5 hours, wherein the inlet pressure is 0.4MPa, the temperature of the oxidation tower is 40 ℃, the aperture of the oxidation column is 5 mu m, the temperature of a heating jacket is controlled to be 60 ℃; when the temperature of steam in a stripping tower is controlled to be 130 ℃, the steam quantity is 300kg/h, the temperature of a water outlet of a heat exchanger is controlled to be 30 ℃, the temperature of a water outlet of a condenser is controlled to be 25 ℃, and the pH value of an intermediate water storage tank is 12, the experiment is carried out through the implementation mode, 795kg/d of byproduct sulfur is effectively recovered in the experiment, 11.2t/d of 15% ammonia water, and both the sulfide and ammonia nitrogen in effluent reach the standard.
Respectively comparing the intake air flow rates to 3m 3 L air, 3m 3 0.6m of oxygen 3 oxygen,/L, 3m 3 The combined gas of/L (0.6 m) 3 Oxygen +2.4m 3 /L nitrogen), 3m 3 The sulfur form in the waste water of thiocarbohydrazide production under the condition of/L ozone. The results of the experiment are shown in table 1:
TABLE 1 comparison of the sulfur obtained under different conditions
Claims (12)
1. A system for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production is characterized by comprising an oxidation part, a filtering part, a pH adjusting part and a stripping tower (9),
the oxidation part comprises an oxidation tower (3) and an aeration column (302) in the oxidation tower, the oxidation tower (3) comprises a waste water inlet, an oxidation gas inlet is connected with the aeration column (302) through an air inlet pipe penetrating through the wall of the oxidation tower (3), the bottom of the oxidation tower (3) is provided with an oxidation liquid outlet,
the filtering part comprises a bag filter, the oxidizing liquid outlet is connected with the inlet of the bag filter, the bottom of the bag filter is provided with a filtrate outlet,
the pH adjusting part comprises a mixer (603), an inlet of the mixer (603) is connected with the filtrate outlet, an outlet of the mixer (603) is connected with an inlet of the stripping tower (9), the top of the stripping tower (9) is provided with an ammonia outlet, and the bottom of the stripping tower (9) is provided with an external water outlet.
2. The system for recovering sulfur and ammonia nitrogen in thiocarbohydrazine production wastewater according to claim 1, wherein the air inlet pipe is in a vertical inverted U shape outside the oxidation tower, and the top of the air inlet pipe is 0-1 m higher than the top of the oxidation tower (3).
3. The system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production according to claim 1, characterized in that the system further comprises a wastewater storage tank (1), wherein an outlet of the wastewater storage tank (1) is connected with the wastewater inlet;
the filtering part also comprises a back washing pipeline connected with the bag filter, and the filtrate outlet is connected with the waste water storage tank (1) through a pipeline.
4. The system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide according to claim 1, wherein the oxidation tower (3) further comprises a jacket (303) arranged at the periphery.
5. The system for recovering sulfur and ammonia nitrogen in waste water from thiocarbohydrazine production according to claim 4, wherein the effective height of the jacket (303) wrapping the oxidation tower (3) is 1/3 to 1/2 of the height of the oxidation tower (3).
6. The system for recovering sulfur and ammonia nitrogen in thiocarbohydrazide production wastewater according to claim 1, wherein the wastewater inlet is positioned between 1/2 to 4/5 of the height of the oxidation tower (3);
the air inlet of the aeration column (302) is positioned between 1/4 to 1/2 of the height of the oxidation tower (3).
7. The system for recovering sulfur and ammonia nitrogen in thio-carbazide production wastewater according to claim 1, wherein the filtering part comprises 2 to 4 groups of bag filters connected in parallel.
8. The system for recovering sulfur and ammonia nitrogen in thiocarbohydrazide production wastewater according to claim 1, wherein the pH adjusting part further comprises an alkali liquor tank (6), and an outlet of the alkali liquor tank (6) is connected with the mixer (603).
9. The system for recovering sulfur and ammonia nitrogen from waste water of thiocarbohydrazide according to claim 1, further comprising an intermediate water storage tank (7), wherein the intermediate water storage tank (7) is located between the mixer (603) and the stripping tower (9).
10. The system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production according to claim 1, characterized in that a heat exchanger (8) is arranged in front of an inlet of the stripping tower (9), and the external water discharged from the stripping tower (9) exchanges heat with the wastewater in front of the stripping tower (9) through the heat exchanger (8).
11. The system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide production according to claim 1, characterized in that the system further comprises a condenser (11), the ammonia gas outlet is connected with the condenser (11), and the outlet of the condenser (11) is connected with an ammonia storage tank (10).
12. The system for recovering sulfur and ammonia nitrogen in wastewater from thiocarbohydrazide according to claim 1, wherein the filtrate outlet is connected with the aeration column (302) through a pipeline and a valve.
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| CN202221414227.7U CN218232078U (en) | 2022-06-08 | 2022-06-08 | System for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production |
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| CN202221414227.7U CN218232078U (en) | 2022-06-08 | 2022-06-08 | System for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production |
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